Polymer electrolyte membrane, membrane electrode assembly and polymer electrolyte water electrolyzer

ABSTRACT

To provide a polymer electrolyte membrane which can be applied to a polymer electrolyte water electrolyzer, and is capable of producing a polymer electrolyte water electrolyzer having a low electrolytic voltage and excellent in hydrogen gas recovery efficiency, as well as a membrane electrode assembly and a polymer electrolyte water electrolyzer obtainable by using it. 
     The polymer electrolyte membrane of the present invention contains a polymer electrolyte, of which the hydrogen gas permeation coefficient under the conditions of a temperature of 80° C. and a relative humidity of 10%, is at most 2.4 x 10 −9  cm 3 .cm/(s.cm 2 .cmHg), wherein the membrane resistance value under the conditions of a temperature of 80° C. and a relative humidity of 50%, is from 50 to 150 mn.cm2.

TECHNICAL FIELD

The present invention relates to a polymer electrolyte membrane, a membrane electrode assembly, and a polymer electrolyte water electrolyzer.

BACKGROUND ART

The polymer electrolyte membrane to be contained in a membrane electrode assembly, is obtainable, for example, by forming a polymer having acid-type sulfonic acid groups into a membrane. In an Example of Patent Document 1, as such a polymer having acid-type sulfonic acid groups, a perfluoropolymer having units represented by —[CF₂—CF(OCF₂CF₂SO₃H)— is disclosed.

A membrane electrode assembly containing a polymer electrolyte membrane can be applied to various applications, and, for example, may be applied to a polymer electrolyte water electrolyzer as disclosed in Patent Document 2 in addition to a polymer electrolyte fuel cell as disclosed in Patent Document 1.

PRIOR ART DOCUMENTS Patent Documents

Patent Document 1: JP-A-2005-082749

Patent Document 2: JP-A-H11-021687

DISCLOSURE OF INVENTION Technical Problem

In recent years, further improvement in performance of a polymer electrolyte water electrolyzer has been required. Specifically, it is required that the electrolytic voltage is low, and the yield of hydrogen generated at the cathode is excellent.

Further, in the polymer electrolyte water electrolyzer, a large pressure is applied to the polymer electrolyte membrane that separates the anode chamber and the cathode chamber. Therefore, the polymer electrolyte membrane may be broken during the operation of the polymer electrolyte water electrolyzer, and depending on the type of the polymer electrolyte membrane, it may not be suitable for use in the polymer electrolyte water electrolyzer.

When the present inventors evaluated the polymer electrolyte membrane containing, as an electrolyte, the above-mentioned perfluoropolymer described in Patent Document 1, they found that there is room for improvement with respect to at least one of the electrolytic voltage and the hydrogen gas yield of the polymer electrolyte water electrolyzer.

In view of the above circumstances, the present invention has an object to provide a polymer electrolyte membrane which can be applied to a polymer electrolyte water electrolyzer, and is capable of producing a polymer electrolyte water electrolyzer having a low electrolytic voltage and being excellent in hydrogen gas yield, as well as a membrane electrode assembly and a polymer electrolyte water electrolyzer obtainable by using it.

Solution to Problem

As a result of diligent studies on the above problem, the present inventors have found that if a polymer electrolyte membrane containing a polymer electrolyte membrane, of which the hydrogen gas permeation coefficient is at most a predetermined value, wherein the membrane resistance value is within a predetermined range, it is possible to apply it to a polymer electrolyte water electrolyzer and to produce a polymer electrolyte water electrolyzer which has a low electrolytic voltage and is excellent in hydrogen gas yield, and thus has arrived at the present invention.

That is, the present inventors have found it possible to solve the above problem by the following constructions.

-   [1] A polymer electrolyte membrane characterized by comprising a     polymer electrolyte, of which the hydrogen gas permeation     coefficient under the conditions of a temperature of 80° C. and a     relative humidity of 10%, is at most 2.4×10⁻⁹ cm³.cm/(s.cm²-cmHg),

wherein the membrane resistance value under the conditions of a temperature of 80° C. and a relative humidity of 50%, is from 50 to 150 mΩ.cm².

-   [2] The polymer electrolyte membrane according to [1], wherein the     polymer electrolyte is a perfluoropolymer having acid-type sulfonic     acid groups. -   [3] The polymer electrolyte membrane according to [2], wherein the     perfluoropolymer contains perfluoromonomer units, and the     perfluoromonomer units contain at least one type of units selected     from the group consisting of perfluorovinyl ether units and     perfluoroallyl ether units. -   [4] The polymer electrolyte membrane according to [2] or [3],     wherein the perfluoropolymer does not substantially contain at least     one type of units selected from the group consisting of units having     a halogen atom other than a fluorine atom, units having a ring     structure, and units having a crosslinked structure consisting of a     covalent bond. -   [5] The polymer electrolyte membrane according to [4], wherein the     perfluoroallyl ether units are units represented by the formula A-1     described later, and in the formula A-1, R^(F1) and R^(F2) are each     independently a C1-3 perfluoroalkylene group. -   [6] The polymer electrolyte membrane according to any one of [3] to     [5], wherein the perfluoromonomer units further contain     tetrafluoroethylene units. -   [7] The polymer electrolyte membrane according to any one of [1] to     [6], wherein the ion exchange capacity of the polymer electrolyte is     from 1.4 to 2.5 meq/g dry resin. -   [8] A membrane electrode assembly characterized by comprising an     anode having a catalyst layer, a cathode having a catalyst layer,     and the polymer electrolyte membrane as defined in any one of [1] to     [7], disposed between the anode and the cathode. -   [9] A polymer electrolyte water electrolyzer characterized by     comprising the membrane electrode assembly as defined in [8].

Advantageous Effects of Invention

According to the present invention, it is possible to provide a polymer electrolyte membrane which can be applied to a polymer electrolyte water electrolyzer, and which is capable of producing a polymer electrolyte water electrolyzer which has a low electrolytic voltage and which is excellent in hydrogen gas yield, as well as a membrane electrode assembly and a polymer electrolyte water electrolyzer obtainable by using it.

BRIEF DESCRIPTION OF DRAWING

FIG. 1 is a schematic cross-sectional view which shows an example of the membrane electrode assembly of the present invention.

DESCRIPTION OF EMBODIMENTS

The following definitions of terms apply throughout the specification and claims unless otherwise specified.

An “ion exchange group” is a group capable of exchanging at least part of ions contained in this group with other ions, and, for example, the following sulfonic acid type functional group and carboxylic acid type functional group may be mentioned.

A “sulfonic acid type functional group” is a general term for an acid-type sulfonic acid group (—SO₃H) and a salt-type sulfonic acid group (—SO₃M², where M² is an alkali metal or a quaternary ammonium cation).

A “carboxylic acid type functional group” is a general term for an acid-type carboxylic acid group (—COOH) and a salt-type carboxylic acid group (—COOM¹, where M¹ is an alkali metal or a quaternary ammonium cation).

The term “does not substantially contain units” is meant that the content of the units relative to all units of the polymer containing the units is at most 1 mol %.

A “unit” in a polymer means an atomic group derived from one molecule of a monomer, formed by polymerization of the monomer. A unit may be an atomic group directly formed by the polymerization reaction, or may be an atomic group having a part of the atomic group changed to another structure by treating the polymer obtained by the polymerization reaction. Further, there may be a case where the structural unit derived from each monomer is described by a term having “unit” added to the monomer name.

A unit represented by the formula A-1 is referred to as a unit A-1. Units represented by other formulas may also be referred to in the same manner.

A compound represented by the formula 1-1 is referred to as a compound 1-1. Compounds represented by other formulas may also be referred to in the same manner.

[Polymer Electrolyte Membrane]

The polymer electrolyte membrane of the present invention (hereinafter simply referred to also as the “electrolyte membrane”) comprises a polymer electrolyte, of which the hydrogen gas permeation coefficient under the conditions of a temperature of 80° C. and a relative humidity of 10%, is at most 2.4×10⁻⁹ cm³.cm/(s.cm².cmHg), wherein the membrane resistance value under the conditions of a temperature of 80° C. and a relative humidity of 50%, is from 50 to 150 mΩ.cm².

According to the electrolyte membrane of the present invention, it is possible to produce a polymer electrolyte water electrolyzer having a low electrolytic voltage and excellent in hydrogen gas yield. The details of this reason have not been clarified yet, but it is presumed to be due to the following reason.

In the polymer electrolyte water electrolyzer, oxygen gas is generated on the anode side and hydrogen gas is generated on the cathode side. When the hydrogen gas generated on the cathode side permeates the electrolyte membrane and moves to the anode side (so-called hydrogen crossover), there arises a problem that the yield of the hydrogen gas of the polymer electrolyte water electrolyzer is lowered

With respect to this problem, the present inventors have found it possible to suppress the occurrence of hydrogen crossover by using an electrolyte membrane comprising a polymer electrolyte, of which the hydrogen gas permeation coefficient is at most a predetermined value, and as a result, it is possible to obtain a polymer electrolyte water electrolyzer excellent in yield of hydrogen.

On the other hand, the present inventors have found that the electrolytic voltage of the polymer electrolyte water electrolyzer can be made to be slightly lower by setting the hydrogen gas permeation coefficient to be at most a predetermined value, but there is room for improvement.

With respect to this problem, the present inventors have found that when an electrolyte membrane, of which the membrane resistance is within a predetermined range, is used, it is possible to obtain a polymer electrolyte water electrolyzer having a low electrolytic voltage. That is, it is assumed that the effect of setting the hydrogen gas permeation coefficient of the polymer electrolyte to be at most a predetermined value and the effect of using an electrolyte membrane, of which the resistance value is within a predetermined range, act synergistically, whereby a polymer electrolyte water electrolyzer wherein the electrolytic voltage is sufficiently low, has been obtained.

<Polymer Electrolyte>

The polymer electrolyte is not particularly limited as long as it is an electrolyte made of a polymer, of which the hydrogen gas permeation coefficient satisfies the range as described later, but from such a viewpoint that the electrolytic voltage of the polymer electrolyte water electrolyzer can be further reduced, and the yield of hydrogen gas will be more excellent, it is preferably a perfluoropolymer having acid-type sulfonic acid groups (hereinafter simply referred to also as “polymer H”).

Polymer H preferably contains perfluoromonomer units from the viewpoint of excellent durability of the electrolyte membrane.

The perfluoromonomer units preferably contain at least one type of units selected from the group consisting of perfluorovinyl ether units and perfluoroallyl ether units (hereinafter simply referred to also as “units A”), since the electrolytic voltage of the polymer electrolyte water electrolyzer can be further reduced.

The units A may contain one or both of perfluorovinyl ether units and perfluoroallyl ether units, but from the viewpoint of easy synthesis, it is preferred that they contain perfluoroallyl ether units, and it is particularly preferred that they are perfluoroallyl ether units.

The units contained in the units A preferably have an ion exchange group, since the membrane resistance of the electrolyte membrane becomes low, and the electrolytic voltage of the polymer electrolyte water electrolyzer can be further reduced, and it is more preferred to have a sulfonic acid type functional group, and It is particularly preferred to have an acid-type sulfonic acid group.

When the respective units contained in the units A have an ion exchange group, the number of ion exchange groups in the respective units is preferably at least 2 from such a viewpoint that the membrane resistance of the electrolyte membrane will be low, and the electrolytic voltage of the polymer electrolyte water electrolyzer can be further reduced, and particularly preferably 2 from such a viewpoint that the synthesis will be easy.

As the perfluoroallyl ether units, units A-1 are preferred, since a polymer electrolyte, of which the hydrogen gas permeation coefficient is in the range described later, and when made into a membrane, the membrane resistance value will be within the range described later, will easily be obtainable.

As the perfluorovinyl ether units, units A-2 or units A-3 are preferred from such a viewpoint that a polymer electrolyte, of which the hydrogen gas permeation coefficient is in the range described later, and when made into a membrane, the membrane resistance value will be within the range described later, will easily be obtainable.

In the formulas A-1 to A-3, R^(F1) and R^(F2) are each independently a C₁₋₃ perfluoroalkylene group.

Specific examples of R^(F1) and R^(F2) may be —CF₂—, —CF₂CF₂—, —CF(CF₃)—, —CF₂CF₂CF₂—, —CF(CF₂CF₃)—, —CF(CF₃)CF₂—, —CF₂CF(CF₃)—, and —C(CF₃)(CF₃)—.

From such a viewpoint that the raw material is inexpensive, from such a viewpoint that the production is easy, and from such a viewpoint that the ion exchange capacity of polymer H can be made to be higher, R^(F1) and R^(F2) are each independently preferably a C_(1 or 2) perfluoroalkylene group. In the case of 2 carbon atoms, a straight chain is preferred. Specifically, —CF₂—, —CF₂CF₂— or —CF(CF₃)— is preferred, —CF₂— or —CF₂CF₂— is more preferred, and —CF₂— is particularly preferred.

In the formula A-2, RF³ is a C₁₋₆ perfluoroalkylene group.

Specific examples of R^(F3) may be —CF₂—, —CF₂CF₂—, —CF(CF₃)—, —CF₂CF₂CF₂—, —CF(CF₂CF₃)—, —CF(CF₃)CF₂—, —CF₂CF(CF₃)—, —C(CF₃)(CF₃)—, and —CF₂CF(CF₃)OCF₂CF (CF₃)—.

From such a viewpoint that the raw material is inexpensive, from such a viewpoint that the production is easy, and from such a viewpoint that the ion exchange capacity of polymer H can be made higher, R^(F3) is preferably a C₁₋₃ perfluoroalkylene group. Specifically, —CF₂—, —CF₂CF₂— or —CF₂CF(CF₃)— is preferred, and —CF₂CF(CF₃)— is particularly preferred.

In the formula A-2, m is 0 or 1.

The perfluoromonomer units may include units other than the units A. As the units other than the units A, perfluoromonomer units which do not have an ion exchange group or its precursor group may be mentioned.

As specific examples of the perfluoromonomer units which do not have an ion exchange group or its precursor group, tetrafluoroethylene (hereinafter referred to also as “TFE”) units and hexafluoropropylene units may be mentioned, and the TFE units are preferred from such a viewpoint that strength of the electrolyte membrane will be excellent.

The lower limit of the content of the units A is, from such a viewpoint that it will be easy to set the ion exchange capacity and the hydrogen gas permeation coefficient of the polymer electrolyte within the ranges described later, and that an electrolyte membrane, of which the membrane resistance value is within the range described later, can be easily obtained, preferably 7 mol %, more preferably 8 mol %, particularly preferably 9 mol %, to all units in polymer H.

The upper limit of the content of the units A is, from such a viewpoint that strength of the electrolyte membrane will be excellent, preferably 45 mol %, more preferably 36 mol %, particularly preferably 22 mol %, to all units in polymer H.

In a case where perfluoromonomer units which do not have an ion exchange group or its precursor group are contained, the content thereof is preferably from 55 to 93 mol %, more preferably from 65 to 92 mol %, particularly preferably 78 to 91 mol %, to all units in polymer H. Such a content is particularly suitable in a case where the perfluoromonomer units are TFE units.

Polymer H preferably does not substantially contain units having a halogen atom other than a fluorine atom (hereinafter referred to also as “units X1”). The chain transfer reaction is thereby less likely to occur at the time of producing polymer H by polymerizing a monomer, and the amount of oligomers formed during the production is less.

Specific examples of the units X1 may be chlorotrifluoroethylene units, bromotrifluoroethylene units, iodotrifluoroethylene units, and dichlorodifluoroethylene units.

“Polymer H does not substantially contain units X” means that the content of the units X1 is at most 1 mol % to all units in polymer H, and it is preferred that polymer H does not contain them (0 mol %).

Polymer H preferably does not substantially contain units having a ring structure (hereinafter referred to also as “units X2”). Polymer H is thereby suppressed from becoming brittle, and the toughness of polymer H will be high, so that the mechanical strength of the electrolyte membrane obtainable by using polymer H will be excellent.

As the ring structure, an aliphatic hydrocarbon ring, an aliphatic heterocycle, an aromatic hydrocarbon ring, or an aromatic heterocycle may be mentioned. The ring structure may be present in the main chain or in the side chain.

As specific examples of the units X2, the units having a cyclic ether structure as described in Japanese Patent No. 4997968 and Japanese Patent No. 5454592 may be mentioned.

The meaning of “polymer H does not substantially contain the units X2” is the same as that with respect to the units X1, and it is preferred that polymer H does not contain the units X2 (0 mol %).

Polymer H preferably does not substantially contain units having a crosslinked structure consisting of a covalent bond (hereinafter referred to also as “units X3”). This makes it easier for polymer H to be dissolved or dispersed in the liquid medium, so that in a case where an electrolyte membrane is to be formed by using the liquid composition containing polymer H and the liquid medium, it will be easy to adjust the membrane thickness of the electrolyte membrane.

The crosslinked structure consisting of a covalent bond means a structure in which a monomer having a crosslinkable group (for example, a vinyl group, a perfluorovinyl group, etc.) that can be crosslinked by a covalent bond is polymerized, and then the crosslinkable group is crosslinked by the covalent bond.

As a specific example of the units X3, units may be mentioned which have a structure such that after polymerizing compounds of the formulas 8 to 15 described in JP-A-2001-176524 (compounds having two crosslinkable groups), a crosslinkable group that was not used in the polymerization, is crosslinked by a covalent bond, or a structure obtainable by crosslinking, at the same time as polymerization reaction, a monomer having a crosslinkable group, crosslinkable by a covalent bond.

The meaning of “polymer H does not substantially contain the units X3” is the same as that with respect to the units X1, and it is preferred that polymer H does not contain the units X3 (0 mol %).

(Method for Producing Polymer Electrolyte)

As an example of the method for producing a polymer electrolyte, the above-mentioned method for producing polymer H will be referred to for the description.

As an example of the method for producing polymer H, a method may be mentioned in which precursor groups of a precursor polymer (hereinafter referred to also as “polymer F”) in which acid-type sulfonic acid groups (specifically groups represented by —SO₂F) in polymer H are precursor groups, are converted to acid-type sulfonic acid groups (—SO₃ ⁻H⁺).

As a specific example of the method of converting the groups represented by —SO₂F being precursor groups, to acid-type sulfonic acid groups, a method may be mentioned in which the groups represented by —SO₂F of polymer F are hydrolyzed to form salt-type sulfonic acid groups, and then, converting the salt-type sulfonic acid groups to an acid-type to form acid-type sulfonic acid groups.

Polymer F is preferably a perfluoropolymer containing perfluoromonomer units and having groups represented by —SO₂F.

The perfluoromonomer units in polymer F preferably contain at least one type of units (hereinafter simply referred to also as “units a”) selected from the group consisting of perfluorovinyl ether units and perfluoroallyl ether units.

The units a may contain one or both of the perfluorovinyl ether units and the perfluoroallyl ether units, but it is preferred that they contain the perfluoroallyl ether units from such a viewpoint that the synthesis is easy, and particularly preferably, they are the perfluoroallyl ether units.

The units contained in the units a may have a precursor group for an ion exchange group or may not have a precursor group for an ion exchange group, but preferably they have a precursor group for an ion exchange group, particularly preferably they have a precursor group for a sulfonic acid type functional group (specifically a group represented by —SO₂F).

As a specific example of the perfluorovinyl ether units in the units a, units may be mentioned in which the acid-type sulfonic acid groups of the perfluorovinyl ether units in the units A as described above are changed to groups represented by —SO₂F.

As the perfluoroallyl ether units in the units a, the units a-1 are preferred.

R^(F1) and R^(F2) in the formula a-1 are, respectively, synonymous with R^(F1) and R^(F2) in the formula A-1.

The perfluoromonomer units in the units a may contain units other than the units a. A specific example of the units other than the units a may be perfluoromonomer units which do not have an ion exchange group or its precursor group.

Specific examples of the perfluoromonomer units which do not have an ion exchange group or its precursor group are the same as those for polymer H.

The contents of the respective units in polymer F are preferably the same as the contents of the respective units in polymer H.

Polymer F preferably does not substantially contain at least one type of units selected from the group consisting of units having a halogen atom other than a fluorine atom, units having a ring structure, and units having a crosslinked structure consisting of a covalent bond, and it is particularly preferred that it does not substantially contain all of these units.

Specific examples of the units having a halogen atom other than a fluorine atom, the units having a ring structure, and the units having a crosslinked structure consisting of a covalent bond, are the same as those in polymer H.

Here, “does not substantially contain” has the same meaning as in the case of polymer H.

The TQ value of polymer F is preferably at least 220° C., more preferably from 225 to 360° C., further preferably from 230 to 350° C. When the TQ value is at least the lower limit value, polymer H having a sufficient molecular weight can be obtained, so that the strength of the electrolyte membrane will be excellent. When the TQ value is at most the upper limit value, the solubility or dispersibility of polymer H in the liquid medium will be improved, so that it will be easy to prepare a liquid composition. The TQ value is an index for the molecular weight of polymer F.

The “TQ value” of polymer F is obtainable by the method as described in the section for Examples given later.

<Physical Characteristics>

The hydrogen gas permeation coefficient of the polymer electrolyte under the conditions of a temperature of 80° C. and a relative humidity of 10% is at most 2.4×10⁻⁹ cm³.cm/(s.cm².cmHg), preferably at most 2.2×10⁻⁹ cm³.cm/(s.cm².cmHg), more preferably at most 2.0×10⁻⁹ cm³.cm/(s.cm².cmHg), particularly preferably at most 1.8×10⁻⁹ cm³.cm/(s.cm².cmHg). When the hydrogen gas permeation coefficient is at most the upper limit value, it is possible to suppress the occurrence of hydrogen crossover.

The hydrogen gas permeation coefficient of the polymer electrolyte under the conditions of a temperature of 80° C. and a relative humidity of 10% is, from such a viewpoint that the resistance value of the electrolyte membrane can be lowered, and the electrolytic voltage of the polymer electrolyte water electrolyzer can be made to be further lowered, preferably at least 1.0×10⁻¹² cm³.cm/(s.cm².cmHg), particularly preferably at least 1.0×10⁻¹¹ cm³.cm/(s.cm2.cmHg).

The “hydrogen gas permeation coefficient” of the polymer electrolyte is obtainable by the method described in the section for Examples given later, by using a membrane having a membrane thickness of 25 μm, made of the polymer electrolyte.

The ion exchange capacity of the polymer electrolyte is preferably from 1.4 to 2.5 meq/g dry resin, more preferably from 1.6 to 2.4 meq/g dry resin, particularly from 1.8 to 2.3 meq/g dry resin. When the ion exchange capacity of the polymer electrolyte is at least the lower limit value, the resistance of the electrolyte membrane obtainable by using it, can be further lowered, and as a result, the electrolytic voltage of the polymer electrolyte water electrolyzer can be made to be further lowered. When the ion exchange capacity of the polymer electrolyte is at most the upper limit value, the strength at the time of being made into the electrolyte membrane will be excellent.

The “ion exchange capacity” of the polymer electrolyte is obtainable by the method as described in the section for Examples given later.

The water content (mass basis) of the polymer electrolyte is preferably from 30 to 300%, particularly preferably from 40 to 200%. When it is at least the lower limit value, the ion conductivity of the electrolyte membrane becomes high, whereby the electrolytic voltage of the polymer electrolyte water electrolyzer can be made to be further lowered. When it is at most the upper limit value, the electrolyte membrane will not be excessively swelled by water, whereby the mechanical strength of the electrolyte membrane will be excellent.

The “water content” of the polymer electrolyte is obtainable by the method described in the section for Examples given later, by using a membrane with a membrane thickness of 25 μm, made of the polymer electrolyte.

The membrane resistance value of the electrolyte membrane under the conditions of a temperature of 80° C. and a relative humidity of 50%, is from 50 to 150 mΩ.cm².

The lower limit value of the membrane resistance value is, from such a viewpoint that the membrane strength can be improved, and it is possible to better prevent formation of cross-over of hydrogen of the polymer electrolyte water electrolyzer, preferably 65 mΩ.cm², more preferably 75 mΩ.cm².

The upper limit value of the membrane resistance value is, from such a viewpoint that the electrolytic voltage of the polymer electrolyte water electrolyzer can be made to be further lower, preferably 135 mΩ.cm², more preferably 125 mΩ.cm².

The “membrane resistance value” of an electrolyte membrane is obtainable by the method described in the section for Examples given later.

The electrical conductivity of the electrolyte membrane under the conditions of a temperature of 80° C. and a relative humidity of 50%, is preferably from 0.08 to 0.16 S/cm, particularly preferably from 0.1 to 0.15 S/cm. When it is at least the lower limit value, the electrolytic voltage of the polymer electrolyte water electrolyzer can be made to be lower. When it is at most the upper limit value, the mechanical durability of the electrolyte membrane will be sufficient.

The “electrical conductivity” of an electrolyte membrane is obtainable by the method described in the section for Examples given later.

The membrane thickness of the electrolyte membrane is preferably from 50 to 200 μm, particularly preferably from 70 to 130 μm. When it is at least the lower limit value, the membrane strength of the electrolyte membrane can be improved, and it is possible to better prevent formation of cross-over of hydrogen. When it is at most the upper limit value, it is possible to better lower the resistance value of the electrolyte membrane, whereby it is possible to make the electrolytic voltage of the polymer electrolyte water electrolyzer to be lower.

The membrane thickness of the electrolyte membrane means an average membrane thickness obtainable by the method described in the section for Examples given later.

<Other Materials>

The electrolyte membrane may be reinforced by a reinforcing material. Specific examples of the reinforcing material may be porous bodies, fibers, woven fabrics and non-woven fabrics.

The reinforcing material is preferably made of a material selected from the group consisting of polytetrafluoroethylene (hereinafter referred to also as “PTFE”), a tetrafluoroethylene-perfluoroalkyl vinyl ether copolymer (hereinafter referred to also as “PFA”), polyetheretherketone (hereinafter referred to also as “PEEK”), and polyphenylene sulfide (hereinafter referred to also as “PPS”).

The electrolyte membrane may contain at least one type of metal, metal compound or metal ion, which contains a metal selected from the group consisting of cerium and manganese, in order to further improve durability. Cerium and manganese will decompose hydrogen peroxide, which is a causative substance that causes degradation of the electrolyte membrane.

The electrolyte membrane may contain silica or heteropolyacid (e.g. zirconium phosphate, phosphomolybdic acid, or phosphotungstic acid), as a water retention agent to prevent drying.

<Application>

The electrolyte membrane is suitably used as a polymer electrolyte membrane for a polymer electrolyte water electrolyzer.

<Method for Producing Electrolyte Membrane>

An example of a method for producing an electrolyte membrane may be a method in which a liquid composition described later is applied to the surface of a base film or a catalyst layer and dried (cast method).

An example of the production method in a case where the electrolyte membrane contains a reinforcing material, may be a method of impregnating the reinforcing material with a liquid composition described later and drying it.

It is preferred to carry out heat treatment in order to stabilize the electrolyte membrane. The temperature for the heat treatment may depend on the type of the polymer electrolyte, but is preferably from 130 to 200° C. When the heat treatment temperature is at least 130° C., the water content of the polymer electrolyte becomes to be proper. When the heat treatment temperature is at most 200° C., the thermal decomposition of sulfonic acid groups will be suppressed, and the excellent conductivity of the electrolyte membrane can be maintained.

The electrolyte membrane may be treated with a hydrogen peroxide solution, if necessary.

(Liquid Composition)

The liquid composition preferably comprises a polymer electrolyte and a liquid medium. The polymer electrolyte in the liquid composition may be dispersed in the liquid medium or may be dissolved in the liquid medium.

As specific examples of the liquid medium, water and an organic solvent may be mentioned. As the liquid medium, only water may be used, only an organic solvent may be used, or a mixed solvent of water and an organic solvent may be used, but it is preferred to use a mixed solvent of water and an organic solvent.

In a case where water is contained as the liquid medium, the dispersibility or solubility of the polymer electrolyte in the liquid medium will easily be improved. In a case where an organic solvent is contained as the liquid medium, an electrolyte membrane which is hardly breakable will easily be obtainable.

As the organic solvent, a C₁₋₄ alcohol is preferred, from such a viewpoint that a hardly breakable electrolyte membrane will easily be obtainable.

As the C₁₋₄ alcohol, for example, methanol, ethanol, 1-propanol, 2-propanol, 1-butanol, 2,2,2-trifluoroethanol, 2,2,3,3,3-pentafluoro-1-propanol, 2,2,3,3-tetrafluoro-1-propanol, 1,1,1,3,3,3-hexafluoro-2- propanol, or 3,3,3-trifluoro-1-propanol may be mentioned.

As the organic solvent, one type may be used alone, or two or more types may be used in combination.

In a case where the liquid medium is a mixed solvent of water and an organic solvent, the content of water is preferably from 10 to 99 mass %, particularly preferably from 20 to 99 mass %, to the total mass of the liquid medium.

In a case where the liquid medium is a mixed solvent of water and an organic solvent, the content of the organic solvent is preferably from 1 to 90 mass %, particularly preferably from 1 to 80 mass %.

When the contents of water and the organic solvent are within the above ranges, an electrolyte membrane having excellent dispersibility or solubility of the polymer electrolyte in the liquid medium and being hardly breakable will easily be obtainable.

The content of the polymer electrolyte is preferably from 1 to 50 mass %, particularly preferably from 3 to 30 mass %, to the total mass of the liquid composition. When it is at least the lower limit value in the above range, a thick membrane can be stably obtained at the time of formation of a membrane. When it is at most the upper limit value in the above range, the viscosity of the liquid composition will become proper.

The liquid composition may contain at least one type of metal, metal compound or metal ion, which contains a metal selected from the group consisting of cerium and manganese, in order to further improve the durability of the electrolyte membrane made from the liquid composition.

[Membrane Electrode Assembly]

The membrane electrode assembly of the present invention comprises an anode having a catalyst layer, a cathode having a catalyst layer, and the above-described electrolyte membrane disposed between the anode and the cathode.

Since the membrane electrode assembly of the present invention contains the above-mentioned electrolyte membrane, it can be applied to a polymer electrolyte water electrolyzer, and the polymer electrolyte water electrolyzer obtainable by using it, will have a low electrolytic voltage and will be excellent in yield of hydrogen gas.

Hereinafter, an example of the membrane electrode assembly of the present invention will be described with reference to the drawing.

FIG. 1 is a cross-sectional view showing an example of the membrane electrode assembly of the present invention. The membrane electrode assembly 10 comprises an anode 13 having a catalyst layer 11 and a gas diffusion layer 12, a cathode 14 having a catalyst layer 11 and a gas diffusion layer 12, and an electrolyte membrane 15 disposed between the anode 13 and the cathode 14, in contact with the catalyst layers 11.

A specific example of the catalyst layer 11 may be a layer containing a catalyst and a polymer having ion exchange groups.

A specific example of the catalyst may be a supported catalyst in which platinum, a platinum alloy or a catalyst containing platinum with a core-shell structure, is supported on a carbon carrier, an iridium oxide catalyst, an alloy containing iridium oxide, and a catalyst containing iridium oxide having a core-shell structure. As the carbon carrier, carbon black powder may be mentioned.

The polymer having ion exchange groups may be a fluorinated polymer having ion exchange groups.

The gas diffusion layer 12 has a function to uniformly diffuse gas in the catalyst layer and a function as a current collector. Specific examples of the gas diffusion layer may be carbon paper, carbon cloth, carbon felt, and a titanium porous material (specifically sintered product of titanium particles or fibers, etc.).

In order to prevent adhesion of the generated gas, the gas diffusion layer may be treated for water-repellency or hydrophilized with PTFE or the like, or may be hydrophilized with a polymer having ion exchange groups or the like.

Although the gas diffusion layer 12 is contained in the membrane electrode assembly in FIG. 1, the gas diffusion layer is an optional component and may not be contained in the membrane electrode assembly.

The electrolyte membrane 15 is an electrolyte membrane (polymer electrolyte membrane) containing the above-mentioned polymer electrolyte.

Specific examples of the method for producing the membrane electrode assembly may be a method in which catalyst layers are formed on an electrolyte membrane and the obtained assembly is further sandwiched between gas diffusion layers, and a method in which a catalyst layer is formed on a gas diffusion layer to form electrodes (anode, cathode), and an electrolyte membrane is sandwiched between the electrodes.

Here, the method for producing the catalyst layer may be a method in which a coating liquid for forming a catalyst layer is applied to a predetermined position and dried as the case requires. The coating liquid for forming a catalyst layer is a liquid having a polymer having ion exchange groups and a catalyst, dispersed in a dispersion medium.

[Polymer Electrolyte Water Electrolyzer]

The polymer electrolyte water electrolyzer of the present invention contains the above-mentioned membrane electrode assembly.

Since the polymer electrolyte water electrolyzer of the present invention contains the above-mentioned membrane electrode assembly, it has a low electrolytic voltage and is excellent in yield of hydrogen gas.

The polymer electrolyte water electrolyzer of the present invention may have a known construction except for using the above-mentioned membrane electrode assembly, and, for example, an embodiment may be mentioned which has an electrolytic cell for setting the membrane electrode assembly, a water supplying means to supply water to the anode side, water recovery means to recover excess water, a gas recovery means to recover generated hydrogen gas, etc., a power source section to apply a voltage, etc.

In the polymer electrolyte water electrolyzer, a voltage is applied between the anode and the cathode of the membrane electrode assembly, and water is supplied to the anode side. The water supplied to the anode side will be decomposed, whereby hydrogen ions and oxygen will be formed. The formed hydrogen ions will be moved to the cathode side via the polymer electrolyte membrane, and will be bonded with electrons at the cathode side to form hydrogen.

EXAMPLES

Hereinafter, the present invention will be described in detail with reference to Examples. Ex. 6-1 to 6-6 and 7-1 to 7-6 are Examples of the present invention, and Ex. 6-7 to 6-21 and 7-7 to 7-21 are Comparative Examples. However, the present invention is not limited to these Examples. Further, the blending amounts of the respective components in Tables given later, are based on mass standard.

[¹H-NMR]

¹H-NMR was measured under the conditions of frequency: 300.4 MHz and chemical shift standard: tetramethylsilane. As the solvent, CD₃CN was used unless otherwise specified. The quantification of the product was carried out from the analysis result of ¹H-NMR and the added amount of the internal standard sample (1,3-bis(trifluoromethyl)benzene).

[¹⁹F-NMR]

¹⁹F-NMR was measured under the conditions of frequency: 282.7 MHz, solvent: CD₃CN, and chemical shift standard: CFCl₃. The quantification of the product was carried out from the analysis result of ¹⁹F-NMR and the added amount of the internal standard sample (1,3-bis(trifluoromethyl)benzene).

[¹³C-NMR]

¹³C-NMR was measured under the conditions of frequency: 75.5 MHz and chemical shift standard: tetramethylsilane. As the solvent, CD₃CN was used unless otherwise specified.

[Ion Exchange Capacity]

A membrane of polymer F or polymer F′ was vacuum-dried at 120° C. for 12 hours. The mass of the membrane of the polymer after drying was measured, and then, the membrane of the polymer was immersed in a 0.85 mol/g sodium hydroxide solution (solvent: water/methanol=10/90 (mass ratio)) at 60° C. for at least 72 hours, to hydrolyze groups represented by —SO2F. The sodium hydroxide solution after the hydrolysis was back-titrated with 0.1 mol/L hydrochloric acid to obtain the ion exchange capacity of polymer F or polymer F′. In the present specification, the ion exchange capacity of polymer H or polymer H′ as a polymer electrolyte is described as being the same as the ion exchange capacity measured by using polymer F or polymer F′ as a precursor.

[Proportions of Respective Units]

The proportions of the respective units in polymer F or polymer F′ were calculated from the ion exchange capacity of polymer F or polymer F′.

The proportions of the respective units in polymer H or polymer H′ are the same as the proportions of the corresponding respective units in polymer F or polymer F′.

[Hydrogen Gas Permeation Coefficient]

The hydrogen gas permeation coefficient of a membrane (membrane thickness: 25 μm) made of polymer H or polymer H′ as a polymer electrolyte was measured in accordance with JIS K 7126-2: 2006 “Plastic-Film and Sheet-Gas Permeability Test Method-Part 2: Isopressure Method” (corresponding to “Annex B (Specification) Test Method by Gas Chromatograph Method” described in International Standard: ISO 1515-2: 2003). As the measuring device, a gas transmittance measuring device (GTR-100XFAG, manufactured by GTR Tech Co., Ltd.) was used.

A membrane made of polymer H or polymer H′ with an effective permeation area of 9.62 cm² was kept at 80° C., and hydrogen gas having a relative humidity of 10% was permitted to flow on a first surface at 30 mL/min, and argon gas having a relative humidity of 10% was permitted to flow on a second surface at 30 mL/min. The hydrogen gas permeating to the argon gas was detected by gas chromatography, and the amount of permeated hydrogen gas as converted to a volume at 25° C. under 1 atm was obtained. Using the obtained amount of hydrogen gas permeated, the permeability of the permeated gas per second per 1 cm² of the membrane area and 1 cmHg of the pressure difference of the permeated gas, was obtained, and the value converted as a 1 cm thick membrane was adopted as the hydrogen gas permeation coefficient. Here, the standard size and membrane thickness of the membrane used in the calculation, were measured under the conditions of temperature: 23° C. and relative humidity: 50% RH.

[Membrane Resistance and Conductivity]

A substrate on which 4-terminal electrodes are arranged at 5 mm intervals is brought into close contact with a polymer electrolyte membrane having a width of 5 mm, and under a constant temperature and constant humidity of temperature: 80° C. and relative humidity: 50% RH, by a known 4-terminal method, the resistance value (membrane resistance value) of the polymer electrolyte membrane was measured under the conditions of AC: 10 kHz and voltage: 1 V, and the conductivity was calculated.

[Water Content]

A membrane made of polymer H or polymer H′ (membrane thickness: 25 μm) was immersed in hot water at 80° C. for 16 hours, and then cooled until the water temperature became at most 25° C. The membrane made of polymer H or polymer H′ was taken out, the water on the surface of the membrane was wiped off with a filter paper, and the mass W1 of the membrane made of polymer H or polymer H′ was measured. After drying the membrane made of polymer H or polymer H′ in a glove box purged with nitrogen for at least 48 hours, the mass W2 of the membrane made of polymer H or polymer H′ was measured in the glove box. The water content (mass basis) was calculated from the following formula I.

Water content (%)=(W1-W2)/W2×100 Formula I

[Hydrogen Leak Amount]

The hydrogen leak amount permeating from the cathode side to the anode side by permeating through the polymer electrolyte membrane of the membrane electrode assembly, is quantified as the oxidation current value of hydrogen on the anode side by the linear sweep voltammetry method. The test is carried out by supplying hydrogen (0.05 mL/min) and nitrogen (0.2 mL/min) to the cathode and anode, respectively, under ambient pressure, and sweeping the potential on the anode side at a sweep rate of 0.5 mV/sec from 0.05 V to 0.5 V using the cathode side as the reference electrode, at a cell temperature of 80° C. and a relative humidity of hydrogen and nitrogen: 100% RH. In the obtainable relationship of the current density to the potential, the value of the intercept of the linear approximation formula in the range of from 0.4 to 0.5 V is taken as the hydrogen leak current value and evaluated in accordance with the following standards. The smaller the hydrogen leak current value, the better the yield of hydrogen gas in the polymer electrolyte water electrolyzer.

◯: The hydrogen leak current value is at most 0.15 mA/cm².

×: The hydrogen leak current value is more than 0.15 mA/cm².

[Electrolytic Voltage]

After heat-treating the membrane electrode assembly at 150° C. for 15 minutes, it was set in the water electrolysis evaluation cell EH50-25 (manufactured by Greenlight innovation).

Next, first, in order to sufficiently hydrate the polymer electrolyte membrane and the ionomer in both electrodes, pure water having a conductivity of at most 1.0 μS/cm, a temperature of 80° C. and a ambient pressure was supplied to the anode side and the cathode side at the flow rate of 50 mL/min for 12 hours. Then, the cathode side was purged with nitrogen.

After nitrogen purging, pure water with a conductivity of at most 1.0 μS/cm and a temperature of 80° C., was supplied to the anode side at a flow rate of 50 mL/min, and while the back pressure was kept to be 100 kPaG for both the anode and cathode, by a large current Potentio/Galvanostat HCP-803 (manufactured by BioLogic), the current was gradually increased by 2.5 A stepwisely in the range from 0 to 32 A (current density from 0 to 2 A/cm²). The current was held for 5 minutes at each stage, and the electrolytic voltage at a current of 32 A (current density 2 A/cm²) was evaluated in accordance with the following standards.

◯: Less than 1.63V

×: At least 1.63V

[Membrane Thickness]

A polymer electrolyte membrane was measured by a digital indicator (manufactured by Mitutoyo Corporation, IDC112X6), and an average thickness was calculated by arithmetically averaging the thicknesses of optional 6 points. Here, the membrane thickness was measured under the conditions of temperature: 23° C. and relative humidity: 50% RH.

[TQ value]

Using a flow tester (CFT-500A, manufactured by Shimadzu Corporation) equipped with a nozzle having a length of 1 mm and an inner diameter of 1 mm, polymer F or F′ was melt extruded by changing the temperature under an extrusion pressure of 2.94 MPa (gauge pressure). A temperature (TQ value) at which the extrusion amount of polymer F or F′ becomes to be 100 mm³/sec was obtained. The higher the TQ value, the larger the molecular weight of the polymer.

[Abbreviations]

TFE: Tetrafluoroethylene,

PSVE: CF₂═CFOCF₂CF(CF₃)OCF₂CF₂SO₂F,

P2SVE: a monomer represented by the following formula m32-1,

sPSVE: CF₂═CFOCF₂CF₂SO₂F,

PFtBPO: (CF₃)₃COOC(CF₃)₃,

AIBN: (CH₃)₂C(CN)N═NC(CH₃)₂(CN),

V-601: CH₃OC(O)C(CH₃)₂—N═N—C(CH₃)₂C(O)OCH₃,

PFB: CF₂CF₂CF₂C(O)OOC(O)CF₂CF₂CF₃,

HFC-52-13p: CF₃(CF₂)₅H,

HFE-347pc-f: CF₃CH₂OCF₂CF₂H,

HCFC-225cb: CClF₂CF₂CHClF,

HCFC-141b: CH3CCl₂F.

Ex. 1 Ex. 1-1

Into a 2 L four-necked flask equipped with a stirrer, a condenser, a thermometer and a dropping funnel, 560 g of chlorosulfonic acid was charged under nitrogen gas sealing. The flask was cooled in an ice bath, and while maintaining the internal temperature to be at most 20° C., a mixed solution of 139.5 g of compound 1-1 and 478.7 g of dichloromethane, was dropwise added over 20 minutes. During the dropwise addition, heat generation and gas generation were observed. After the dropwise addition was completed, the flask was set in an oil bath, and the reaction was conducted for 7 hours while maintaining the internal temperature to be from 30 to 40° C. The reaction proceeded with the generation of gas, and a white solid was precipitated.

After the reaction, the pressure inside the flask was reduced, and dichloromethane was distilled off. A yellowish white solid remained in the flask. The solid was analyzed by ¹H-NMR, whereby it was confirmed that compound 2-1 was formed.

NMR spectrum of compound 2-1:

¹H-NMR (solvent: D₂O): 4.27 ppm (—CH₂—, 4H, s).

¹³C-NMR (solvent: D₂O): 62.6 ppm (—CH₂—), 195.3 ppm (C═O).

Ex. 1-2

Compound 2-1 obtained in Ex. 1-1 was used directly in the next reaction without being isolated. Into the flask in Ex. 1, 2,049 g of thionyl chloride was added. The flask was heated to 80° C. and refluxed for 15 hours. As the reaction progressed, the reflux temperature increased from 52° C. to 72° C. Gas generation was confirmed during the reaction. The point at which compound 2-1 was all dissolved, and gas generation was subsided, was taken as the reaction end point. The reaction solution was transferred to a 2 L separable flask, and left to cool for 9 hours while the gas phase was sealed with nitrogen gas, whereby a dark brown solid was precipitated in the separable flask. By decantation, unreacted thionyl chloride was removed. Toluene was added to wash the precipitated solid, and again by decantation, the toluene was removed. Toluene washing was carried out a total of 3 times, and the total amount of toluene used was 1,207 g. The precipitated solid was dried at 25° C. for 71 hours under a nitrogen gas stream. The solid after the drying was collected and was analyzed by ¹H-NMR, whereby it was confirmed that 356.5 g of compound 3-1 with a purity of 96.2% was obtained. The yield based on compound 1-1 became to be 56.0%.

NMR spectrum of compound 3-1:

¹H-NMR: 5.20 ppm (—CH₂—, 4H, s).

¹³C-NMR: 72.3 ppm (—CH₂—), 184.6 ppm (C═O).

Ex. 1-3

Into a 1 L four-necked flask equipped with a stirrer, a condenser and a thermometer, 90.0 g of compound 3-1 and 750 mL of acetonitrile were charged under nitrogen gas sealing. The flask was cooled in an ice bath, and 110.3 g of potassium hydrogen fluoride was added with stirring. The heat generation associated with the addition was slight. The ice bath was changed to a water bath, and the reaction was carried out for 62 hours while maintaining the internal temperature to be from 15 to 25° C. Along with the reaction, a fine white solid was produced. The reaction solution was transferred to a pressure filter, and unreacted potassium hydrogen fluoride and the product were separated by filtration. Acetonitrile was added to the filter, and the separated solid was washed until the filtrate became transparent, whereupon the washing solution was recovered. The filtrate and washing solution were subjected to an evaporator to distill off acetonitrile. 950 mL of toluene was added to the solid remaining after the drying, and the mixture was heated to 100° C. to dissolve the solid in toluene. The dissolved solution was filtered by gravity filtration to remove undissolved components. The filtrate was transferred to a 1 L separable flask, and left to cool for 14 hours while the gas phase was sealed with nitrogen gas, whereby pale brown acicular crystals were precipitated in the separable flask. The crystals were washed with toluene and dried at 25° C. for 30 hours under a nitrogen gas stream. The solid after the drying was recovered and analyzed by ¹H-NMR and ¹⁹F-NMR, whereby it was confirmed that 58.1 g of compound 4-1 with a purity of 97.6% was obtained. The yield based on compound 3-1 became to be 72.3%.

NMR spectrum of compound 4-1:

¹H-NMR: 4.97 ppm (—CH₂—, 4H, d, J=3.1 Hz).

¹⁹F-NMR: 62.4 ppm (—SO₂F, 2F, t, J=3.1 Hz).

¹³C-NMR: 60.7 ppm (—CH₂—), 184.9 ppm (C═O).

Ex. 1-4

Into a 200 mL nickel autoclave, 9.93 g of compound 4-1 and 89.7 g of acetonitrile were charged. The autoclave was cooled, and while maintaining the internal temperature to be from 0 to 5° C., nitrogen gas was fed at a flow rate of 6.7 L/hr, whereupon the reaction solution was bubbled for 1 hour. While maintaining the temperature of the reaction solution to be from 0 to 5° C., a mixed gas of fluorine gas and nitrogen gas (mixing ratio =10.3 mol %/89.7 mol %) was introduced at a flow rate of 6.7 L/hr over 6 hours. Nitrogen gas was fed again at a flow rate of 6.7 L/hr, and the reaction solution was bubbled for 1 hour. From the autoclave, 103.2 g of the reaction solution was recovered. The reaction solution was quantitatively analyzed by ¹⁹F-NMR, whereby it was confirmed that compound 5-1 was contained at 8.4 mass %. The reaction yield based on compound 4-1 became to be 66%.

NMR spectrum of compound 5-1:

¹⁹F-NMR: -104.1 ppm (—CF₂—, 4F, s), 45.8 ppm (—SO₂F, 2F, s).

Ex. 1-5

Into a 200 mL nickel autoclave, 19.9 g of compound 4-1 and 85.6 g of acetonitrile were charged. The autoclave was cooled, and while maintaining the internal temperature to be from 0 to 5° C., nitrogen gas was fed at a flow rate of 6.7 L/hr, whereupon the reaction solution was bubbled for 1 hour. While maintaining the temperature of the reaction solution to be from 0 to 5° C., a mixed gas of fluorine gas and nitrogen gas (mixing ratio=10.3 mol %/89.7 mol %) was introduced at a flow rate of 16.4 L/hr over 6.5 hours. Nitrogen gas was again fed at a flow rate of 6.7 L/hr, and the reaction solution was bubbled for 1 hour. From the autoclave, 109.6 g of the reaction solution containing compound 5-1 was recovered.

Ex. 1-6

Into a 200 mL nickel autoclave, 20.1 g of compound 4-1 and 80.1 g of acetonitrile were charged. The autoclave was cooled, and while maintaining the internal temperature to be from 0 to 5° C., nitrogen gas was fed at a flow rate of 6.7 L/hr, whereupon the reaction solution was bubbled for 1 hour. While maintaining the temperature of the reaction solution to be from 0 to 5° C., a mixed gas of fluorine gas and nitrogen gas (mixing ratio=20.0 mol %/80.0 mol %) was introduced at a flow rate of 8.4 L/hr over 6 hours. Nitrogen gas was again fed at a flow rate of 6.7 L/hr, and the reaction solution was bubbled for 1 hour. From the autoclave, 107.1 g of the reaction solution containing compound 5-1 was recovered.

Ex. 1-7

Into a 50 mL four-necked flask equipped with a stirrer, a condenser, a thermometer and a dropping funnel, 1.65 g of potassium fluoride and 7.8 mL of diethylene glycol dimethyl ether (diglyme) were charged. The flask was cooled in an ice bath, and while maintaining the internal temperature to be from 0 to 10° C. with stirring, 8.43 g of the reaction solution obtained in Ex. 1 to 4 was dropwise added by using a plastic syringe. Strong heat generation was confirmed, and it took 15 minutes for the dropwise addition. After the dropwise addition was completed, the ice bath was replaced with a water bath, and the reaction was carried out to be from 15 to 20° C. for 1 hour. The flask was again cooled in an ice bath, and while maintaining the temperature of the reaction solution to be from 0 to 10° C., from the dropping funnel, 6.56 g of compound 6-1 was dropwise added. After the dropwise addition was completed, the ice bath was replaced with a water bath and the reaction was carried out to be from 20 to 25° C. for 3.5 hours. A by-product solid was removed from the reaction solution by suction filtration, and the filtrate was recovered. The filtered residual solid was washed with a suitable amount of acetonitrile, and the washing liquid was mixed with the filtrate. 37.1 g of the filtrate was quantitatively analyzed by ¹⁹F-NMR, whereby it was confirmed that compound 7-1 was contained in an amount of 2.04 mass %. The reaction yield based on compound 4-1 became to be 46.6%.

NMR spectrum of compound 7-1:

¹⁹F-NMR: -191.5 ppm (CF₂═CF—, 1F, ddt, J=116, 38, 14 Hz), −133.8 ppm (—O—CF—, 1F, tt, J=21.3, 6.1Hz), −103.1 ppm (—CF₂—SO₂F, 4F, m), −101.5 ppm (CF₂═CF—, 1F, ddt, J=116, 49, 27Hz), −87.6 ppm (CF₂═CF—, 1F, ddt, J=49, 38, 7 Hz), −67.5 ppm (—CF₂—O—, 2F, m), 46.8 ppm (—SO₂F, 2F, s).

Ex. 1-8

Into a 500 mL four-necked flask equipped with a stirrer, a condenser, a thermometer and a dropping funnel, 36.6 g of potassium fluoride and 125.6 g of acetonitrile were charged. The flask was cooled in an ice bath, and while maintaining the internal temperature to be from 0 to 10° C. with stirring, 79.8 g of the reaction solution obtained in Ex. 1-5 was dropwise added by using a plastic dropping funnel. Strong heat generation was confirmed, and it took 23 minutes for the dropwise addition. After the dropwise addition was completed, the ice bath was replaced with a water bath, and the reaction was carried out to be from 20 to 30° C. for 5.5 hours. The flask was again cooled in an ice bath, and while maintaining the temperature of the reaction solution to be from 0 to 10° C., 146.0 g of compound 6-1 was dropwise added from the dropping funnel. After the dropwise addition was completed, the ice bath was replaced with a water bath, and the reaction was carried out to be from 15 to 25° C. for 16 hours. In the same manner as in Ex. 1-7, suction filtration was conducted, and 412.3 g of the obtained filtrate was quantitatively analyzed by ¹⁹F-NMR, whereby it was confirmed that compound 7-1 was contained in an amount of 3.93 mass %. The reaction yield based on compound 4-1 became to be 55.9%. By vacuum distillation of the filtrate, compound 7-1 was isolated as a fraction with a boiling point of 97.2° C/10 kPa. The gas chromatographic purity was 98.0%.

Ex. 1-9

Into a 50 mL four-necked flask equipped with a stirrer, a condenser, a thermometer and a dropping funnel, 3.70 g of potassium fluoride and 10.9 g of acetonitrile were charged. The flask was cooled in an ice bath, and while maintaining the internal temperature to be from 0 to 10° C. with stirring, 10.2 g of the reaction solution obtained in Ex. 1-6 was dropwise added by using a plastic syringe. Strong heat generation was confirmed, and it took 8 minutes for the dropwise addition. After the dropwise addition was completed, the ice bath was replaced with a water bath, and the reaction was carried out to be from 20 to 30° C. for 3 hours. The flask was again cooled in an ice bath, and while maintaining the temperature of the reaction solution to be from 0 to 10° C., 14.6 g of compound 6-1 was dropwise added from the dropping funnel. After the dropwise addition was completed, the ice bath was replaced with a water bath, and the reaction was carried out to be from 15 to 25° C. for 17 hours. In the same manner as in Ex. 1-7, suction filtration was conducted, and 55.9 g of the obtained filtrate was quantitatively analyzed by ¹⁹F-NMR, whereby it was confirmed that compound 7-1 was contained in an amount of 4.77 mass %. The reaction yield based on compound 4-1 became to be 69.6%. Further, the reaction yield based on compound 1-1 (reaction yield over the entire monomer synthesis step) became to be 28.2%.

Ex. 2 Ex. 2-1

Into an autoclave (internal volume: 100 mL, made of stainless steel), 70.0 g of compound 7-1 was put, cooled with liquid nitrogen, and degassed. 2.53 g of TFE was introduced into the autoclave and heated in an oil bath until the internal temperature reached 100° C. The pressure at that time was 0.29 MPaG (gauge pressure). A mixed solution of 36.3 mg of PFtBPO as a polymerization initiator and 2.58 g of HFC-52-13p was injected into the autoclave. Further, nitrogen gas was introduced from the injection line, and the injection liquid in the injection line was completely pushed in. By this operation, TFE in the gas phase was diluted, and as a result, the pressure increased to 0.56 MPaG. While maintaining the pressure at 0.56 MPaG, polymerization was carried out by continuously adding TFE. When the amount of TFE added reached 4.03 g in 9.5 hours, the inside of the autoclave was cooled to stop the polymerization, and the gas in the system was purged. The reaction solution was diluted with HFC-52-13p, HFE-347pc-f was added, and the polymer was precipitated and filtered. Then, the operation of stirring the polymer in HFC-52-13p and reprecipitating it with HFE-347pc-f was repeated twice. Vacuum drying was conducted at 120° C. to obtain polymer F-1 being a copolymer of TFE and compound 7-1. Using the obtained polymer F-1, the above-mentioned various physical properties were measured. The results are shown in Table 1.

Ex. 2-2

The respective conditions in Ex. 2-1 were changed as shown in Table 1. However, in Ex. 2-2, the initial charging of TFE was not conducted, and, instead, after heating to the polymerization temperature, TFE was charged to the pressure before the nitrogen gas dilution shown in Table 1. Except for this, polymer F-2 was obtained in the same manner as in Ex. 2-1. Using the obtained polymer F-2, the above-mentioned various physical properties were measured. The results are shown in Table 1.

TABLE 1 Ex. 2-1 Ex. 2-2 Reactor volume [mL] 100 100 Compound 7-1 [g] 70.0 80.0 Initial charge of TFE [g] 2.53 — HFC-52-13p [g] 2.58 4.23 Type of polymerization initiator PFtBPO PFtBPO Amount of polymerization initiator [mg] 36.3 41.4 Polymerization temperature [° C.] 100 100 Pressure before nitrogen gas dilution [MPaG] 0.29 0.29 Polymerization pressure [MPaG] 0.56 0.56 Continuously added TFE [g] 4.03 5.59 Polymerization time [hr] 9.5 6.9 Type of polymer F F-1 F-2 Yield of polymer F [g] 6.4 8.47 Compound 7-1 units [mol %] 13.8 12.4 TFE units [mol %] 86.2 87.6 Ion exchange capacity 1.87 1.74 [meq/g dry resin] TQ value [° C.] 238 298

Ex. 3 Ex. 3-1

Using polymer F-1, a membrane of polymer H-1 was obtained by the following method.

Polymer F-1 was press-molded at a temperature higher by 10° C. than the TQ value and 4 MPa (gauge pressure) to obtain a membrane of polymer F-1. The membrane of polymer F-1 was immersed in an alkaline aqueous solution A (potassium hydroxide/water=20/80 (mass ratio)) at 80° C. for 16 hours to hydrolyze —SO₂F of polymer F-1 and convert it to —SO₃K. Further, the membrane of the polymer was immersed in a 3 mol/L hydrochloric acid aqueous solution at 50° C. for 30 minutes, and then immersed in ultrapure water at 80° C. for 30 minutes. The cycle of immersion in hydrochloric acid aqueous solution and immersion in ultrapure water, was carried out a total of 5 times to convert —SO₃K of the polymer to —SO₃H. Washing with ultrapure water was repeated until the pH of the water in which the membrane of the polymer was immersed became 7. The membrane of the polymer was sandwiched between filter papers and air-dried to obtain a membrane of polymer H-1.

Ex. 3-2

A membrane of polymer H-2 was obtained in the same manner as in Ex. 3-1 except that instead of polymer F-1, polymer F-2 was used, and instead of the alkaline aqueous solution A, an alkaline aqueous solution C (potassium hydroxide/methanol/water =15/20/65 (mass ratio)) was used.

Ex. 4 Ex. 4-1

Into a Hastelloy autoclave having an internal volume of 230 mL,123.8 g of PSVE, 35.2 g of HCFC-225cb and 63.6 mg of AIBN were put, cooled with liquid nitrogen, and degassed. The temperature was raised to 70° C., TFE was introduced into the system, and the pressure was maintained at 1.14 MPa (gauge pressure). TFE was continuously added so that the pressure became constant at 1.14 MPa (gauge pressure). After 7.9 hours, when the amount of TFE added reached 12.4 g, the autoclave was cooled, and the gas in the system was purged to terminate the reaction. The polymer solution was diluted with HCFC-225cb, then HCFC-141b was added for precipitation. After washing with HCFC-225cb and HCFC-141b, the mixture was dried to obtain 25.1 g of polymer F′-1 being a copolymer of TFE and PSVE. The results are shown in Table 2.

Ex. 4-2 to Ex. 4-3

TFE and sPSVE or P2SVE were copolymerized in the same manner as in Ex. 4-1 except that the respective conditions in Ex. 4-1 were changed as shown in Table 2, to obtain polymer F′-2 or F′-3. The results are shown in Table 3-1 to Table 3-2.

TABLE 2 Ex. 4-1 Ex. 4-2 Ex. 4-3 Reactor volume [mL] 230 125 2500 Type of monomer having a −SO₂F group PSVE sPSVE P2SVE Content of monomer having a −SO₂F group 123.8 85.0 1786.3 HFCF-225cb [g] 35.26.9 112.0 Type of polymerization initiator AIBN PFB V-601 Amount of polymerization initiator [mg] 63.6 25.59 190.0 Polymerization temperature [° C.] 70 24 66 Polymerization pressure [MPaG] 1.14 0.47 1.11 Polymerization time [hr] 7.9 10.0 4.0 Type of polymer F′ F′-1 F′-2 F-3 Yield of polymer F′ [g] 25.1 4.2 198.4 Monomer units having a −SO₂F group 17.7 19.5 16.1 [mol %] TFE units [mol %] 82.3 80.5 83.9 Ion exchange capacity 1.10 1.45 1.75 [meq/g dry resin] TQ value [° C.] 225 333 237

Ex. 5 Ex. 5-1

A membrane of polymer H′-1 was obtained in the same manner as in Ex. 3-1 except that polymer F′-1 was used instead of polymer F-1.

Ex. 5-2

A membrane of polymer H′-2 was obtained in the same manner as in Ex. 3-1 except that polymer F′-2 was used instead of polymer F-1.

Ex. 5-3

A membrane of polymer H′-3 was obtained in the same manner as in Ex. 3-1 except that polymer F′-3 was used instead of polymer F-1.

Ex. 6 Ex. 6-1

Into a 100 mL container made of polytetrafluoroethylene (PTFE), 4.3 g of a finely cut polymer H-1 membrane and 75 g of ultrapure water were added, and heated at 200° C. for 24 hours. The content was transferred to a PTFE container and air-dried at 30° C. for 64 hours in a nitrogen atmosphere. The dried polymer H-1 was transferred to a 200 mL glass autoclave, and 21.4 g of a mixed solvent of ultrapure water/ethanol (50/50 (mass ratio)) was added. After stirring at 110° C. for 25 hours, 3.87 g of ultrapure water was added for dilution. After stirring at 90° C. for 5 hours, the mixture was left to cool and filtered by means of a pressure filter (filter paper: manufactured by Advantec Toyo Kaisha, Ltd., PF040), to obtain 31.9 g of a liquid composition S-1 having polymer H-1 dispersed in the mixed solvent.

The liquid composition S-1 was applied on a 100 μm ethylene-tetrafluoroethylene copolymer (ETFE) sheet by a die coater to form a membrane, which was dried at 80° C. for 15 minutes, and further dried at 185° C. for 30 minutes to obtain a polymer electrolyte membrane 1 made of a membrane of polymer H being an electrolyte. The amount of the liquid composition applied was adjusted so that the membrane thickness of the polymer electrolyte membrane became to have the value as shown in Tables 3-1 to 3-2. The results are shown in Table 3-1.

Ex. 6-2 to 6-22

In the same manner as in Ex. 6-1 except that a liquid composition is prepared by using polymer H or polymer H′ as shown in Tables 3-1 to 3-2 instead of the polymer H-1, and the coating amount of the liquid composition was adjusted so that the membrane thickness of the polymer electrolyte membrane became to have the value as shown in Tables 3-1 to 3-2, polymer electrolyte membranes 2 to 21 made of a membrane of polymer H or H′, were obtained.

Here, In Tables 3-1 to 3-2, polymer H′-4 means Nafion (registered trademark) 117 (manufactured by DuPont, an electrolyte membrane having a thickness of 180 μm made of a perfluoropolymer containing TFE units and PSVE units). Polymer H′-5 means Nafion (registered trademark) 115 (manufactured by DuPont, an electrolyte membrane having a thickness of 130 μm made of a perfluoropolymer containing TFE units and PSVE units). Polymer H′-6 means Nafion (registered trademark) 212 (manufactured by DuPont, an electrolyte membrane having a thickness of 50 μm made of a perfluoropolymer containing TFE units and PSVE units).

The results are shown in Tables 3-1 to 3-2.

TABLE 3-1 Ex. 6-1 Ex. 6-2 Ex. 6-3 Ex. 6-4 Ex. 6-5 Ex. 6-6 Ex. 6-7 Ex. 6-8 Ex. 6-9 Ex. 6-10 Ex. 6-11 Type of polymer H-1 H-1 H-1 H-2 H-2 H-2 H-1 H-1 H-2 H-2 H-1 Ion exchange 1.87 1.87 1.87 1.74 1.74 1.74 1.87 1.87 1.74 1.74 1.10 capacity of polymer H or polymer H′ [meq/g dry resin] Moisture content 152 152 152 93 93 93 152 152 93 93 49 of membrane made of polymer H or H′ [%] Hydrogen gas 2.10E−09 2.10E−09 2.10E−09 1.60E−09 1.60E−09 1.60E−09 2.10E−09 2.10E−09 1.60E−09 1.60E−09 5.50E−09 permeation coefficient of membrane made of polymer H or polymer H′ [cm³ · cm/ (s · cm² · cmHg)] Type of polymer 1 2 3 4 5 6 7 8 9 10 11 electrolyte membrane Membrane 76 91 114 81 98 122 38 189 41 203 200 resistance value of polymer electrolyte membrane [mΩ · cm²] Conductivity of 0.132 0.132 0.132 0.123 0.123 0.123 0.132 0.132 0.123 0.123 0.05 polymer electrolyte membrane [S/cm] Membrane 100 120 150 100 120 150 50 250 50 250 100 thickness of polymer electrolyte membrane [μm]

TABLE 3-2 Ex. 6-12 Ex. 6-13 Ex. 6-14 Ex. 6-15 Ex. 6-16 Ex. 6-17 Ex. 6-18 Ex. 6-19 Ex. 6-20 Ex. 6-21 Type of polymer H′-1 H′-2 H′-2 H′-2 H′-3 H′-3 H′-3 H′-4 H′-5 H′-6 Ion exchange 1.10 1.45 1.45 1.45 1.75 1.75 1.75 1.00 1.00 1.00 capacity of polymer H or polymer H′ [meq/g dry resin] Moisture content 49 80 80 80 138 138 138 42 42 42 of membrane made of polymer H or H′ [%] Hydrogen gas 5.50E−09 3.85E−09 3.85E−09 3.85E−09 3.70E−09 3.70E−09 3.70E−09 4.40E−09 4.40−09 4.40E−09 permeation coefficient of membrane made of polymer H or polymer H′ [cm³ · cm/ (s · cm² · cmHg)] Type of polymer 12 13 14 15 16 17 18 19 20 21 electrolyte membrane Membrane 300 132 158 197 74 89 111 391 283 109 resistance value of polymer electrolyte membrane [mΩ · cm²] Conductivity of 0.05 0.076 0.076 0.076 0.135 0.135 0.135 0.046 0.046 0.046 polymer electrolyte membrane [S/cm] Membrane 150 100 120 150 100 120 150 180 130 50 thickness of polymer electrolyte membrane [μm]

In Tables 3-1 to 3-2, the description such as “2.10E-09” is an abbreviation for exponential notation. As a specific example, “2.10E-09” means “2.10×10⁻⁹”. The same applies to Tables 4-1 to 4-2 given later.

Ex. 7 Ex. 7-1

A polymer (ion exchange capacity: 1.10 meq/g dry resin) obtained by copolymerizing TFE and PSVE, followed by hydrolysis and acid treatment to form an acid type, was dispersed in a solvent of water/ethanol =40/60 (mass %) at a solid content concentration of 25.8% to obtain a dispersion (hereinafter referred to also as “dispersion X”). Ethanol (0.52 g) and water (3.34 g) were added to the obtained dispersion X (19.0 g), and further an iridium oxide catalyst (manufactured by Tanaka Kikinzoku Kogyo) (13.0 g) having a specific surface area of 100 m²/g containing 76 mass % of iridium was added into the dispersion. The obtained mixture was treated by a planetary bead mill (rotation speed: 300 rpm) for 30 minutes, then water (4.49 g) and ethanol (4.53 g) were added, and further treated with a planetary bead mill (rotation speed: 200 rpm) for 60 minutes to obtain an anode catalyst ink having a solid content concentration of 40 mass %.

On the ETFE sheet, the anode catalyst ink was applied by an applicator so that the iridium content became to be 1.0 mg/cm², dried at 80° C. for 10 minutes, and further heat-treated at 150° C. for 15 minutes to obtain an anode catalyst layer decal.

Water (59.4 g) and ethanol (39.6 g) were added to a supported catalyst (“TEC10E50E”, manufactured by Tanaka Kikinzoku Kogyo) (11 g) in which 46 mass % of platinum was supported on carbon powder, and mixed and pulverized by using an ultrasonic homogenizer to obtain a dispersion of the catalyst.

To the dispersion of the catalyst, a mixed liquid (29.2 g) in which dispersion X (20.1 g), ethanol (11 g) and Zeorora-H (manufactured by Zeon Corporation) (6.3 g) were mixed and kneaded in advance, was added. Further, water (3.66 g) and ethanol (7.63 g) were added to the obtained dispersion and mixed for 60 minutes by using a paint conditioner to adjust the solid content concentration to be 10.0 mass %, then a cathode catalyst ink was obtained.

The cathode catalyst ink was applied onto an ETFE sheet by a die coater, dried at 80° C., and further heat-treated at 150° C. for 15 minutes to obtain a cathode catalyst layer decal having a platinum content of 0.4 mg/cm².

By letting one surface of a polymer electrolyte membrane 1 face the surface where the anode catalyst layer of the anode catalyst layer decal exists, and letting the other surface of the electrolyte membrane face the surface where the catalyst layer of the cathode catalyst layer decal exists, the anode catalyst layer, the polymer electrolyte membrane 1 and the cathode catalyst layer were bonded by hot-pressing at a press temperature of 150° C. for a press time of 10 minutes and a pressure of 3 MPa, and after lowering the temperature to 70° C., the pressure was released. The ETFE sheets of the anode catalyst layer decal and the cathode catalyst layer decal were peeled off to obtain a membrane electrode assembly having an electrode area of 16 cm². The obtained membrane electrode assembly was used for evaluation of electrolytic voltage and hydrogen leakage amount. The results are shown in Table 4-1.

Ex. 7-2 to 7-21

In the same manner as in Ex. 7-1 except that the polymer electrolyte membranes 2 to 21 shown in Tables 4-1 to 4-2 were used instead of the polymer electrolyte membrane 1 obtained in Ex. 6-1, membrane electrode assemblies to be used for evaluation of the electrolytic voltage and the amount of hydrogen leakage were prepared. The results are shown in Tables 4-1 to 4-2.

TABLE 4-1 Ex. 7-1 Ex. 7-2 Ex. 7-3 Ex. 7-4 Ex. 7-5 Ex. 7-6 Ex. 7-7 Ex. 7-8 Ex. 7-9 Ex. 7-10 Type of polymer 1 2 3 4 5 6 7 8 9 10 11 electrolyte membrane Electrolytic voltage ∘ ∘ ∘ ∘ ∘ ∘ — x — x x Hydrogen leak amount ∘ ∘ ∘ ∘ ∘ ∘ — ∘ — ∘ x

Ex. Ex. Ex. Ex. Ex. Ex. Ex. Ex. Ex. Ex. 7-12 7-13 7-14 7-15 7-16 7-174 7-18 7-19 7-20 7-21 Type of polymer 12 13 14 15 16 17 18 19 20 21 electrolyte membrane Electrolytic voltage x ∘ x x ∘ ∘ ∘ x x ∘ Hydrogen leak amount x x x x x x x x x x

In the above Tables 4-1, the symbol “-” in electrolytic voltage and hydrogen leak amount, means that the polymer electrolyte membrane was broken during the evaluation, whereby the evaluation was impossible.

As shown in Tables 3-1 to 3-2 and Tables 4-1 to 4-2, when a polymer electrolyte membrane containing a polymer electrolyte, of which the hydrogen gas permeation coefficient under the conditions of a temperature of 80° C. and a relative humidity of 10% was at most 2.4×10⁻⁹ cm³.cm/(s.cm².cmHg) and the membrane resistance value under the conditions of a temperature of 80° C. and a relative humidity of 50%, is from 50 to 150 mΩ.cm², was used, a polymer electrolyte water electrolyzer having a low electrolytic voltage and being excellent in yield of hydrogen gas, was obtained (Ex. 6-1 to 6-6 and Ex. 7-1 to 7-6).

On the other hand, when a polymer electrolyte membrane in which at least one of the hydrogen gas permeation coefficient and the membrane resistance value was out of the above range, was used, at least one of the electrolytic voltage and the yield of hydrogen gas, was inferior (Ex. 6-8, 6-10 to 6-21, 7-8 and 7-10 to 7-21).

Further, when a polymer electrolyte membrane, of which the membrane resistance value was less than the above-mentioned range, was used, the polymer electrolyte membrane was broken during the evaluation, whereby it was not possible to conduct evaluations of the electrolytic voltage and hydrogen leak amount, and it was found to be difficult to apply it to a polymer electrolyte water electrolyzer (Ex. 6-7, 6-9, 7-7 and 7-9).

This application is a continuation of PCT Application No. PCT/JP2020/008346, filed on Feb. 28, 2020, which is based upon and claims the benefit of priority from Japanese Patent Application No. 2019-036692 filed on Feb. 28, 2019. The contents of those applications are incorporated herein by reference in their entireties.

REFERENCE SYMBOLS

10: Membrane electrode assembly

11: Catalyst layer

12: Gas diffusion layer

13: Anode

14: Cathode

15: Electrolyte membrane 

What is claimed is:
 1. A polymer electrolyte membrane characterized by comprising a polymer electrolyte, of which the hydrogen gas permeation coefficient under the conditions of a temperature of 80° C. and a relative humidity of 10%, is at most 2.4×10⁻⁹ cm³.cm/(s.cm².cmHg), wherein the membrane resistance value under the conditions of a temperature of 80° C. and a relative humidity of 50%, is from 50 to 150 mΩ.cm².
 2. The polymer electrolyte membrane according to claim 1, wherein the polymer electrolyte is a perfluoropolymer having acid-type sulfonic acid groups.
 3. The polymer electrolyte membrane according to claim 2, wherein the perfluoropolymer contains perfluoromonomer units, and the perfluoromonomer units contain at least one type of units selected from the group consisting of perfluorovinyl ether units and perfluoroallyl ether units.
 4. The polymer electrolyte membrane according to claim 2, wherein the perfluoropolymer does not substantially contain at least one type of units selected from the group consisting of units having a halogen atom other than a fluorine atom, units having a ring structure, and units having a crosslinked structure consisting of a covalent bond.
 5. The polymer electrolyte membrane according to claim 4, wherein the perfluoroallyl ether units are units represented by the formula A-1:

in the formula A-1, R^(F1) and R^(F2) are each independently a C₁₋₃ perfluoroalkylene group.
 6. The polymer electrolyte membrane according to claim 3, wherein the perfluoromonomer units further contain tetrafluoroethylene units.
 7. The polymer electrolyte membrane according to claim 1, wherein the ion exchange capacity of the polymer electrolyte is from 1.4 to 2.5 meq/g dry resin.
 8. A membrane electrode assembly characterized by comprising an anode having a catalyst layer, a cathode having a catalyst layer, and the polymer electrolyte membrane as defined in claim 1, disposed between the anode and the cathode.
 9. A polymer electrolyte water electrolyzer characterized by comprising the membrane electrode assembly as defined in claim
 8. 